Process for producing hydrofluoroolefin

ABSTRACT

To provide a method for producing a hydrofluoroolefin, wherein formation of an over-reduced product having hydrogen added to a material chlorofluoroolefin and an over-reduced product having not only chlorine atoms but also fluorine atoms in the chlorofluoroolefin replaced with hydrogen atoms, as by-products, is suppressed. 
     A method for producing a hydrofluoroolefin, which comprises reacting a specific chlorofluoroolefin with hydrogen in the presence of a catalyst supported on a carrier, to obtain a specific hydrofluoroolefin,
         wherein the catalyst is a catalyst composed of an alloy containing at least one platinum group element selected from the group consisting of palladium and platinum, and at least one second element selected from the group consisting of manganese, copper, aluminum, gold, lithium, sodium, potassium, magnesium, silver, zinc, cadmium, indium, silicon, germanium, tin, lead, arsenic, antimony and bismuth.

TECHNICAL FIELD

The present invention relates to a method for producing ahydrofluoroolefin.

BACKGROUND ART

2,3,3,3-Tetrafluoropropene (CF₃CF═CH₂) (hereinafter sometimes referredto as “HFO-1234yf), which contains no chlorine, is useful as analternative to Freon such as a chlorofluorocarbon to be used as arefrigerant, etc.

As a method for producing HFO-1234yf, a method may be mentioned in which1,1-dichloro-2,2,3,3,3-pentafluoropropane (CF₃CF₂CHCl₂) (hereinaftersometimes referred to as “HCFC-225ca”) is subjected todehydrofluorination to obtain 1,1-dichloro-2,3,3,3-tetrafluoropropene(CF₃CF═CCl₂) (hereinafter sometimes referred to as “CFO-1214ya”), andthe obtained CFO-1214ya is reduced by reaction with hydrogen to obtainHFO-1234yf.

As a method of reducing CFO-1214ya to obtain HFO-1234yf, for example,the following method (i) disclosed in Patent Document 1 may bementioned. (i) A method of subjecting CFO-1214ya and a hydrogen gas to areaction represented by the following formula (6) in the presence of apalladium catalyst supported on alumina, at from 100 to 400° C.,preferably from 125 to 350° C.:

CF₃CF=CCl₂+2H₂→CF₃CF=CH₂+2HCl  (6)

However, by the reaction represented by the above formula (6),1,1,1,2-tetrafluoropropane (CF₃CHFCH₃) (hereinafter sometimes referredto as “HFC-254eb”) and 3,3,3-trifluoropropene (CF₃CH═CH₂) (hereinaftersometimes referred to as “HFO-1243zf”) which are over-reduced productsform as by-products.

If over-reduced products form in a large amount, the yield of the aimedproduct decreases, and the production efficiency decreases. Further,HFO-1243zf has a boiling point close to that of the aimed HFO-1234yf,and is thereby hardly separated and removed by subsequent distillation.Accordingly, HFO-1243zf will remain as an impurity in HFO-1234yfobtainable by distillation, and a separation and purification step isadditionally required to obtain a high purity product.

Further, Patent Document 2 discloses the following method (ii) as amethod of carrying out a reduction reaction similarly. (ii) A method ofreacting RfCF═CX₂ (wherein Rf is a C₁₋₁₀ fluoroalkyl group, and X ischlorine, bromine or iodine) with hydrogen at from 5 to 200° C. in thepresence of a palladium catalyst supported on activated carbon to obtainRfCF═CH₂.

However, in the method (ii) also, RfCH═CH₂which is an over-reducedproduct forms as a by-product together with the aimed RfCF═CH₂. Forexample, in a case where Rf is CF₃—, that is, in a case where the aimedproduct is HFO-1234yf, the over-reduced product is hardly separated fromthe aimed product by distillation in the same manner as the method (i).

Further, as a method for reducing chlorine in a chlorofluoroolefin,Patent Document 3 discloses the following method (iii). (iii) A methodof subjecting chlorotrifluoroethylene and a hydrogen gas to a reactionrepresented by the following formula (9) in the presence of a palladiumcatalyst supported on activated carbon at from 100 to 350° C.,preferably from 200 to 250° C.:

CF₂=CClF+H₂→CF₂=CHF+HCl   (9)

Further, Patent Document 4 discloses the following method (iv). (iv) Amethod of subjecting 1,2-dichlorodifluoroethylene and a hydrogen gas toa reaction represented by the following formula (10) in the presence ofa palladium catalyst supported on activated carbon at from 150 to 600°C., preferably from 200 to 400° C.:

CClF=CClF+2H₂→CHF=CHF+2HCl   (10)

However, in the methods (iii) and (iv) also, in addition to the aimedproduct, an over-reduced product will form as a by-product, whereby theimpurity of the aimed product will decrease.

PRIOR ART DOCUMENTS Patent Documents

Patent Document 1: W02008/060614

Patent Document 2: JP-A-H2-286635

Patent Document 3: W02012/000853

Patent Document 4: JP-A-H1-287044

DISCLOSURE OF INVENTION Technical Problem

It is an object of the present invention to provide a method forproducing a hydrofluoroolefin, by a reaction of replacing chlorine atomsin a material chlorofluoroolefin with hydrogen atoms to produce ahydrofluoroolefin, wherein formation of an over-reduced product havinghydrogen added to the chlorofluoroolefin and an over-reduced producthaving not only chlorine atoms but also fluorine atoms in thechlorofluoroolefin replaced with hydrogen atoms, as by-products, issuppressed.

Solution to Problem

The present invention provides the following [1] to [14]. [1] A methodfor producing a hydrofluoroolefin, which comprises reacting achlorofluoroolefin represented by the following formula (1) withhydrogen in the presence of a catalyst supported on a carrier, to obtaina hydrofluoroolefin represented by the following formula (2),

wherein the catalyst is a catalyst composed of an alloy containing atleast one platinum group element selected from the group consisting ofpalladium and platinum, and at least one second element selected fromthe group consisting of manganese, copper, aluminum, gold, lithium,sodium, potassium, magnesium, silver, zinc, cadmium, indium, silicon,germanium, tin, lead, arsenic, antimony and bismuth:

CZX═CClY  (1)

wherein X is a fluorine atom or a chlorine atom, Y is a fluorine atom, achlorine atom or a hydrogen atom, and Z is a fluorine atom or CF₃;

CZX′═CHY′  (2)

wherein X′ is a fluorine atom when X is a fluorine atom, or X′ is ahydrogen atom when X is a chlorine atom, Y′ is a fluorine atom when Y isa fluorine atom, or Y′ is a hydrogen atom when Y is a chlorine atom or ahydrogen atom, and Z is the same as Z in the formula (1). [2] The methodfor producing a hydrofluoroolefin according to [1], wherein the secondelement is at least one member selected from the group consisting ofcopper, gold, tin, antimony and bismuth. [3] The method for producing ahydrofluoroolefin according to [1] or [2], wherein the content ratio ofthe platinum group element to the second element (platinum groupelement:second element) in the alloy is from 60:40 to 99:1 by massratio. [4] The method for producing a hydrofluoroolefin according to anyone of [1] to [3], wherein the catalyst is a catalyst composed of analloy of palladium and at least one second element selected from thegroup consisting of copper, gold, tin, antimony and bismuth. [5] Themethod for producing a hydrofluoroolefin according to any one of [1] to[4], wherein the carrier is at least one member selected from the groupconsisting of activated carbon, carbon black and carbon fibers.

[6] The method for producing a hydrofluoroolefin according to any one of[1] to [4], wherein the carrier is at least one member selected from thegroup consisting of alumina, silica, titania and zirconia. [7] Themethod for producing a hydrofluoroolefin according to any one of [1] to[6], wherein the amount of the alloy catalyst supported is from 0.1 to10 mass % based on the carrier. [8] The method for producing ahydrofluoroolefin according to any one of [1] to [7], wherein thechlorofluoroolefin and hydrogen are introduced to a catalyst layerpacked with the carrier supporting the catalyst, and reacted in agaseous phase. [9] The method for producing a hydrofluoroolefinaccording to [8], wherein the chlorofluoroolefin and hydrogen areintroduced to a gas introduction part of the catalyst layer, andhydrogen is introduced from at least one point between the gasintroduction part and a gas discharge part of the catalyst layer. [10]The method for producing a hydrofluoroolefin according to [8] or [9],wherein the reaction is carried out while the maximum temperature of thecatalyst layer is controlled to be at most 130° C. [11] The method forproducing a hydrofluoroolefin according to any one of [8] to [10],wherein the proportion of hydrogen to the chlorofluoroolefin introducedto the catalyst layer is from 0.1 to 0.7 as represented by the ratio(H₂/Cl) of the total number of moles of hydrogen to the number of molesof chlorine atoms in the chlorofluoroolefin.

[12] The method for producing a hydrofluoroolefin according to any oneof [1] to [7], wherein the chlorofluoroolefin and hydrogen are reactedin a liquid phase in the presence of the carrier supporting thecatalyst. [13] The method for producing a hydrofluoroolefin according toany one of [1] to [12], wherein the chlorofluoroolefin is at least onemember selected from the group consisting of chlorotrifluoroethylene,trans-1,2-dichloro-1,2-difluoroethylene,cis-1,2-dichloro-1,2-difluoroethylene,1,1-dichloro-2,3,3,3-tetrafluoropropene and1-chloro-2,3,3,3-tetrafluoropropene. [14] The method for producing ahydrofluoroolefin according to any one of [1] to [12], wherein2,3,3,3-tetrafluoropropene is produced from1,1-dichloro-2,3,3,3-tetrafluoropropene.

Advantageous Effects of Invention

According to the production method of the present invention, formationof an over-reduced product having not only chlorine atoms but alsofluorine atoms in a material chlorofluoroolefin replaced with hydrogenatoms as a by-product is suppressed, whereby the aimed hydrofluoroolefincan be obtained easily with high purity.

BRIEF DESCRIPTION OF DRAWING

FIG. 1 is a view schematically illustrating a reaction apparatus used inExamples.

DESCRIPTION OF EMBODIMENTS

[Method for Producing Hydrofluoroolefin]

The present invention provides a method for producing ahydrofluoroolefin, which comprises reacting a chlorofluoroolefinrepresented by the above formula (1) with hydrogen in the presence of acatalyst supported on a carrier, to obtain a hydrofluoroolefinrepresented by the above formula (2).

Further, the catalyst used in the production method is a catalystcomposed of an alloy containing at least one platinum group elementselected from the group consisting of palladium and platinum, and atleast one second element selected from the group consisting ofmanganese, copper, aluminum, gold, lithium, sodium, potassium,magnesium, silver, zinc, cadmium, indium, silicon, germanium, tin, lead,arsenic, antimony and bismuth.

(Material and Reaction Product)

The present invention provides a method comprising reacting thechlorofluoroolefin represented by the above formula (1) with hydrogen toproduce the hydrofluoroolefin represented by the above formula (2).

Now, the chlorofluoroolefin represented by the above formula (1) whichis one of the materials, and the reaction product obtained by using thechlorofluoroolefin, will be described.

<Chlorofluoroolefin>

The chlorofluoroolefin which is one of the materials in the presentinvention is a compound represented by the above formula (1). Among thechlorofluoroolefins represented by the formula (1), in that a formedproduct is expected as an environmentally friendly alternativerefrigerant having a high refrigerating efficiency, preferred ischlorotrifluoroethylene, trans-1,2-dichloro-1,2-difluoroethylene,cis-1,2-dichloro-1,2-difluoroethylene, CFO-1214ya or1-chloro-2,3,3,3-tetrafluoropropene (hereinafter sometimes referred toas “HCFO-1224yd”). Further, a mixture of CFO-1214ya and HCFO-1224yd isalso preferred.

Hereinafter, a trans-form of geometrical isomers will be represented byadding the prefix (E) to a compound name or a chemical formula, and acis-form will be represented by adding the prefix (Z) to a compound nameor a chemical formula.

Chlorotrifluoroethylene can be produced by dechlorination of1,1,2-trichloro-1,2,2-trifluoroethane or heat decomposition ofchlorodifluoromethane and dichlorofluoromethane.

(E)-1,2-dichloro-1,2-difluoroethylene and(Z)-1,2-dichloro-1,2-difluoroethylene can be produced by heatdecomposition of dichlorofluoromethane.

CFO-1214ya can be produced by a known method. For example, a method ofbringing HCFC-225ca into contact with an aqueous alkali solution in thepresence of a phase transfer catalyst to conduct dehydrofluorination maybe mentioned. For the reaction, dichloropentafluoropropane (hereinaftersometimes referred to as “HCFC-225”) containing HCFC-225ca may be used,and only HCFC-225ca in HCFC-225 is selectively subjected todehydrofluorination by the phase transfer catalyst. After the reaction,CFO-1214ya can be separated and recovered by a known method such asdistillation.

The above HCFC-225 containing HCFC-225ca can be produced by reactingtetrafluoroethylene and dichlorofluoromethane in the presence of acatalyst such as aluminum chloride. HCFC-225 obtained by the reactioncontains as the main component HCFC-225ca and1,3-dichloro-1,2,2,3,3-pentafluoropropane (CHClFCF₂CClF₂) (hereinaftersometimes referred to as “HCFC-225cb”) and further contains a smallamount of 2,2-dichloro-1,1,3,3,3-pentafluoropropane (CHF₂CCl₂CF₃,hereinafter sometimes referred to as “HCFC-225aa”),2,3-dichloro-1,1,2,3,3-pentafluoropropane (CHF₂CClFCClF₂, hereinaftersometimes referred to as “HCFC-225bb”) and the like.

As the HCFC-225 containing HCFC-225ca, a commercial product may be used.As a commercial product, ASAHIKLIN (trademark) AK225 (manufactured byAsahi Glass Company, Limited, a mixture comprising 48 mol % ofHCFC-225ca and 52 mol % of HCFC-225cb, hereinafter referred to as“AK225”) may, for example, be mentioned.

The phase transfer catalyst is preferably tetrabutylammonium bromide(TBAB).

HCFO-1224yd is formed as an intermediate when CFO-1214ya and hydrogenare reacted to obtain HFO-1234yf.

<Reaction Product>

The aimed reaction product obtainable by the production method of thepresent invention is a compound represented by the above formula (2).X′, Y′ and Z in the above formula (2) correspond to X, Y and Z in thechlorofluoroolefin represented by the above formula (1) which is one ofthe materials.

When X in the above formula (1) is a fluorine atom, X′ is a fluorineatom. When X is a chlorine atom, X′ is a hydrogen atom.

When Y in the above formula (1) is a fluorine atom, Y′ is a fluorineatom. When Y is a chlorine atom or a hydrogen atom, Y′ is a hydrogenatom.

Z in the above formula (1) is the same as Z in the above formula (1).

For example, in a case where the material chlorofluoroolefin ischlorotrifluoroethylene, trifluoroethylene obtained by a reactionrepresented by the following formula (3) is the aimed reaction product.

CFCl=CF₂+H₂→CHF=CF₂+HCl   (3)

In a case where the material chlorofluoroolefin is1,2-dichloro-1,2-difuoroethylene, 1,2-difluoroethylene obtained byreactions represented by the following formulae (4) and (5) is the aimedreaction product.

(E)−CFCl=CFCl+2H₂→(E)−CHF=CHF+2HCl   (4)

(Z)−CFCl=CFCl+2H₂→(Z)−CHF=CHF+2HCl   (5)

In a case where the material chlorofluoroolefin is CFO-1214ya,HCFO-1224yd obtained by a reaction represented by the following formula(6) is the aimed reaction product.

CF₃CF=CCl₂+2H₂→CF₃CF=CH₂+2HCl   (6)

In a case where the material chlorofluoroolefin is HCFO-1224yd,HFO-1234yf obtained by a reaction represented by the following formula(7) is the aimed reaction product.

CF₃CF=CHCl+H₂→CF₃CF=CH₂+HCl  (7)

(Catalyst)

The catalyst in the present invention is composed of an alloy containinga specific platinum group element and the second element.

<Alloy>

The specific platinum group element in the present invention is at leastone platinum group element selected from the group consisting ofpalladium and platinum. In a case where either one of palladium andplatinum is employed, the palladium or platinum forms an alloy with thesecond element. Further, in a case where both palladium and platinum areemployed, the palladium and platinum may be in the form of a mixture orin the form of an alloy. In the case of a mixture, at least one ofpalladium and platinum forms an alloy with the second element. In thecase of an alloy of palladium and platinum, said alloy will be referredto as a palladium/platinum alloy.

A catalyst composed of palladium has a higher degree of conversion and ahigher selectivity in a hydrogen reduction reaction. On the other hand,a catalyst composed of platinum has higher acid resistance and a longercatalyst life. With a view to enjoying properties of both of them, it ispreferred to use, as the specific platinum group element, both palladiumand platinum, more preferably a palladium/platinum alloy.

Hereinafter, unless otherwise specified, the platinum group elementmeans the above specific platinum group element, and its simplesubstance will be referred to as a platinum group metal.

The second element is at least one member selected from the groupconsisting of manganese, copper, aluminum, gold, lithium, sodium,potassium, magnesium, silver, zinc, cadmium, indium, silicon, germanium,tin, lead, arsenic, antimony and bismuth.

If the reaction of the present invention is carried out using a simplesubstance of the above platinum group element as the catalyst, thehydrogen reducing activity of the platinum group metal tends to be toohigh, and an over-reduced product is likely to form as a by-product. Onthe other hand, when an alloy of the platinum group element and thepredetermined second element is used as the catalyst, the hydrogenreducing activity of the platinum group metal is suppressed, andformation of an over-reduced product as a by-product is suppressed.Further, by using an alloy, the durability of the catalyst will alsoimprove.

In order to further suppress formation of an over-reduced product as aby-product and to improve the durability of the catalyst, it is morepreferred to conduct alloy solid-solubilization of the alloy of theplatinum group element and the second element by heat treatment in aninert gas atmosphere of e.g. a nitrogen gas or an argon gas or in areducing atmosphere containing a very small amount of hydrogen, wherebythe platinum group element and the second element are formed into analloy in a more uniform state.

The second element is preferably at least one member selected from thegroup consisting of manganese, copper, aluminum, gold, silver, zinc,cadmium, indium, silicon, germanium, tin, lead, arsenic, antimony andbismuth, which is less reactive with water, and is more preferably atleast one member selected from the group consisting of manganese,copper, aluminum, gold, silver, zinc, indium, silicon, germanium, tin,antimony and bismuth, in view of reduced influence over the environmentand low toxicity. Since the hydrogen reduction reaction involvesdehydrochlorination, the periphery of the catalyst packed in the reactoris in an acidic atmosphere. Accordingly, by the catalyst having acidresistance, the catalyst will have high durability, and further,excessive hydrogen reducing activity of the platinum group metal can bereduced to prepare the aimed hydrofluoroolefin with a high selectivity,and accordingly among the above more preferred additional elements,further preferred is at least one member selected from the groupconsisting of copper, gold, tin, antimony and bismuth, particularlypreferred is at least one member selected from the group consisting ofcopper, tin, antimony and bismuth.

The content ratio of the platinum group element to the second element(platinum group element: second element) in the alloy is preferably from60:40 to 99:1 by mass ratio, with a view to further suppressingformation of an over-reduced product as a by-product.

The catalyst may contain, as an element other than the platinum groupelement and the second element, for example, a metal element such asiron, cobalt or nickel, and such an element may be contained in the formof an alloy with the platinum group element or the second element. Suchan element other than the platinum group element and the second elementmay be used alone or in combination of two or more.

In a case where an element other than the platinum group element and thesecond element is contained, the content ratio of “the element otherthan the platinum group element and the second element” is preferablyfrom 0.01 to 20 parts by mass per 100 parts by mass of the total amountof the platinum group element and the second element.

<Carrier>The catalyst is used as supported on a carrier. It is preferredto use the carrier to dispersibly support the alloy.

The carrier may, for example, be a carbon material such as activatedcarbon, carbon black or carbon fibers, or an oxide-based material suchas alumina, silica, titania or zirconia. Particularly, preferred isactivated carbon or alumina, which has a relatively large specificsurface area and which readily support the alloy, and more preferred isactivated carbon, with which formation of an over-reduced product as aby-product can be further suppressed.

As the activated carbon, for example, activated carbon prepared fromwood, charcoal, fruit shell such as coconut shell, peat, lignite, coalor the like may be mentioned.

As the shape of the activated carbon, aggregates of briquette with alength at a level of from 2 to 5 mm, shot at a level of from 4 to 50mesh or granular charcoal may, for example, be mentioned. Among them,the above aggregates of briquette or shot at a level of from 4 to 20mesh is preferred.

As alumina, α-alumina, γ-alumina, θ-alumina, etc. differing in thecrystalline state may be mentioned. Alumina may be widely selected fromγ-alumina having a relatively large specific surface area to highlycrystalline α-alumina having a small specific surface area. It ispreferred to use a formed alumina carrier, which is formed into spheresor pellets, in order that the reaction tube is easily packed with thecatalyst and the material gas will smoothly flow.

The amount of the alloy catalyst supported is preferably from 0.1 to 10mass %, more preferably from 0.5 to 1.0 mass % based on the carrier.When the amount of the catalyst supported is at least the lower limit,the reactivity of the chlorofluoroolefin and hydrogen will improve, andwhen it is at most the upper limit, an excessive temperature increase ofthe catalyst layer by the heat of reaction will be suppressed andformation of an over-reduced product as a by-product tends to besuppressed and in addition, the catalyst will readily be available.

The specific surface area of the catalyst-supporting carrier ispreferably from 10 to 2,000 m²/g, more preferably from 100 to 1,500m²/g. When the specific surface area of the catalyst-supporting carrieris at least the lower limit, the reactivity of the chlorofluoroolefinand hydrogen will more improve, and when it is at most the upper limit,formation of an over-reduced product as a by-product will be furthersuppressed.

The specific surface area of the catalyst-supporting carrier is measuredby a method in accordance with a N₂gas adsorption method, for example, aBET method.

(Method for Producing Catalyst-Supporting Carrier)

The catalyst-supporting carrier may be produced by a known method. Forexample, an impregnation method or a colloid method may, for example, bementioned.

The impregnation method is the most common method as a method forproducing the catalyst-supporting carrier. A catalyst metal saltsolution is brought into contact with the carrier to let the salt of thecatalyst metal be adsorbed on the surface of the carrier, theimpregnated carrier is dried, and then a reducing agent is brought intocontact with the metal salt on the surface of the carrier to reduce themetal salt to let the catalyst metal component be supported on thesurface of the carrier. The reducing agent may be a reducing compoundsuch as ammonia, hydrazine or sodium borohydride, a reducing gas such ashydrogen, an alcohol, an aldehyde, an organic acid or its salt, boronhydride or its salt, or a reducing liquid such as a hydrazine.

By the colloid method, a metal fine particle dispersion is adsorbed onthe surface of the carrier, followed by drying to obtain carrierparticles supporting metal fine particles. The metal fine particledispersion is obtained by dissolving a metal salt in a solvent andreducing the metal salt by a reducing agent. A polymer organic compoundmay be used as a protecting agent so as to improve dispersibility of themetal fine particles, or may not be used. A commonly used protectingagent is polyvinylpyrrolidone, polyethyleneimine, polyallylamine,poly(N-carboxymethyl)allylamine, poly(N,N-dicarboxymethyl) allylamine,poly(N-carboxymethyl)ethyleneimine, or the like.

(Reaction)

The reaction may be conducted in a gaseous phase or in a liquid phase solong as the above catalyst is used.

As the reaction method, the following method (α) or (β) may bementioned. Method (α): the chlorofluoroolefin and hydrogen are reactedin a gaseous phase in the presence of the catalyst. Method (β): thechlorofluoroolefin and hydrogen are reacted in a liquid phase in thepresence of the catalyst.

<Method (α)>

The method (a) may, for example, be a method in which thechlorofluoroolefin and hydrogen are introduced to a reactor packed withthe catalyst-supporting carrier and reacted in a gaseous phase. Themethod may, for example, be specifically a method in which a gascontaining a chlorofluoroolefin gas and a hydrogen gas (hereinaftersometimes referred to as “a material mixture gas”) is introduced to thereactor, followed by reaction.

The catalyst layer is obtained by packing the reactor with theabove-described catalyst-supporting carrier. The packing density of thecatalyst-supporting carrier is preferably from 0.5 to 1 g/cm³, morepreferably from 0.6 to 0.8 g/cm³. When the packing density is at leastthe lower limit, the amount of the catalyst-supporting carrier packedper unit volume tends to be large, and the gas amount to be reacted canbe increased, whereby the productivity will improve. On the other hand,when it is at most the upper limit, the temperature of the catalystlayer will not be too increased as described hereinafter, and theafter-described maximum temperature of the catalyst layer tends to bemaintained at the desired temperature or below.

As the reactor, a typical flow reactor used for a gas-solidheterogeneous catalytic reaction in which the catalyst-supportingcarrier is a solid and the reaction fluid is a gas may be used. Such aflow reactor is roughly classified into a fixed bed reactor and afluidized bed reactor. The fixed bed reactor is packed with a formedproduct of the catalyst-supporting carrier so as to reduce the pressureloss of the reaction fluid. Further, a system in which the reactor ispacked with the catalyst-supporting carrier in the same manner as thefixed bed reactor, the catalyst-supporting carrier is let to move bygravitation, withdrawn from the bottom of the reactor and regenerated,is called a moving bed reactor.

In the fluidized bed reactor, an operation is carried out such that thecatalyst layer behaves as if it is a fluid by the reaction fluid,whereby the catalyst-supporting carrier particles move in the reactor assuspended in the reaction fluid.

In the present invention, either the fixed bed reactor or the fluidizedbed reactor may be used, however, in order to suppress deterioration ofthe catalyst without decreasing the selectivity of the catalyticreaction, the fixed bed reactor capable of properly controlling thereaction temperature is preferred. As the fixed bed reactor, there are atubular reactor and a tank reactor, and a tubular reactor is preferablyused in view of controllability of the reaction temperature. Further, ashell and tube heat exchanger comprising many reaction tubes having asmall tube diameter arranged in parallel, and a heating mediumcirculating over the reaction tubes may, for example, be employed. In acase where more than one reactor is provided in series, more than onecatalyst layer is provided.

At least one stage of the catalyst layer is necessary, and two or morestages may be provided.

If the reaction temperature in the catalyst layer decreases, thereactivity of the catalyst decreases. Accordingly, it is preferred tokeep the reaction temperature in the catalyst layer to be a desiredtemperature so as to maintain a high reactivity. In order to keep thereaction temperature in the catalyst layer to be a desired temperature,for example, a method of heating the catalyst layer from outside e.g. bya heat medium may be mentioned.

The chlorofluoroolefin and hydrogen react usually in a part of theregion of the catalyst layer (hereinafter referred to as “reactionregion”). In a case where the reaction temperature in the catalyst layeris kept to be a desired temperature, usually, the temperature on theupstream side in the reaction zone in the catalyst layer is maintainedby heating. In this specification, the temperature on the upstream sidein the reaction region maintained by heating will be referred to as “thetemperature of the catalyst layer”.

The temperature of the catalyst layer is kept to be a temperature higherthan the dew point of the material mixture gas in order that thereaction is a gaseous phase reaction.

For example, in a case where CFO-1214ya having a boiling point of 46° C.is used as the chlorofluoroolefin, considering the reactivity, thetemperature of the catalyst layer is preferably at least 50° C., morepreferably at least 60° C. Further, in a case where HCFO-1224yd havingan estimated boiling point of from 15 to 17° C. is used as thechlorofluoroolefin, the temperature of the catalyst layer is preferablyat least 20° C., more preferably at least 30° C.

The catalyst usually deteriorates with time as the reaction proceeds.The reaction zone originates from the introduction part of the materialmixture gas at the beginning of the reaction. With deterioration of thecatalyst at the introduction part of the material mixture gas with timeas the reaction proceeds, the reaction zone moves toward the downstreamside in the gas flow direction.

Since a high temperature produced gas formed in the reaction zone flowsinto the vicinity on the downstream side in the reaction zone, thevicinity on the downstream side is usually at the highest temperature inthe catalyst layer. In this specification, the temperature of the regionat the highest temperature in the catalyst layer will be referred to as“the maximum temperature of the catalyst layer”. The temperature on thefurther downstream side of the vicinity on the downstream side decreasesfrom the maximum temperature of the catalyst layer with an increase ofthe distance from the reaction zone.

As a method of measuring the maximum temperature of the catalyst layer,for example, a measurement method using a bulk thermometer may bementioned. As described above, since the reaction zone moves toward thedownstream side in the gas flow direction, the region indicating themaximum temperature of the catalyst layer also moves together with themovement of the reaction zone. Accordingly, the measurement part of abulk thermometer is preliminarily disposed in the gas introduction partof the catalyst layer, and after the beginning of the reaction, themeasurement part is moved to the downstream side in the gas flowdirection as the reaction proceeds, whereby the maximum temperature ofthe catalyst layer can be measured.

In this specification, “the gas introduction part” means a point wherethe material mixture gas is introduced in the catalyst layer.

With a view to suppressing formation of an over-reduced product as aby-product, the reaction is carried out preferably while the maximumtemperature of the catalyst layer is controlled to be at most 130° C.,more preferably at most 100° C. By controlling the maximum temperatureof the catalyst layer to be at most the upper limit, an excesstemperature increase of the catalyst layer due to the heat of reactioncan be suppressed.

As a method of keeping the maximum temperature of the catalyst layer tobe a desired temperature, a method of introducing hydrogen to thecatalyst layer dividedly (method (α1)) may be mentioned. By the method(α1), a high productivity is likely to be maintained while the maximumtemperature of the catalyst layer is controlled to be a desiredtemperature or lower.

In the method (α1), the number of hydrogen introduction point is notparticularly limited, and may be 2 or more. A case where the number ofhydrogen introduction point is 2 may be a case where one point in thegas introduction part from which hydrogen contained in the materialmixture gas is introduced and one point from which only a hydrogen gasis introduced (hereinafter referred to as “hydrogen introduction part”),i.e. totally 2 points are provided.

In view of simplification of the process, the number of the hydrogenintroduction point is preferably 2. In order that the reaction zone inthe catalyst layer can be dispersed without changing the amount of thechlorofluoroolefin introduced, and that generation of the heat ofreaction is prevented from being concentrated in one point, wherebylocal excessive heat generation in the catalyst layer can be suppressedwithout decreasing the productivity, the number of the hydrogenintroduction point is preferably at least 3.

In a case where hydrogen is introduced dividedly, it is preferred toevenly divide and introduce hydrogen to the respective points, wherebythe reaction zone is dispersed and the maximum temperature of thecatalyst layer is likely to be kept low.

In a case where the hydrogen introduction part is provided, a method(α1-1) may be mentioned in which a mixture gas of a part of hydrogen andthe entire amount of the chlorofluoroolefin to be introduced to thecatalyst layer, as the material mixture gas, is introduced from the gasintroduction part (located on the most upstream side in the gas flowdirection) of the catalyst layer, and the rest of hydrogen is introducedfrom at least one hydrogen introduction part on the downstream side ofthe gas introduction part. By such a method, in addition to the gasflowing from the upstream side (usually the produced gas after a part ofthe chlorofluoroolefin is reacted with hydrogen), hydrogen is furtherintroduced from the hydrogen introduction part, and this hydrogen reactswith the unreacted chlorofluoroolefin on the downstream side from thehydrogen introduction part. The produced gas after sufficient reactionof the chlorofluoroolefin and hydrogen is discharged from the gasdischarge part located on the most downstream side in the gas flowdirection of the catalyst layer.

In the method (α1-1), it is preferred that between the gas introductionpart and the first hydrogen introduction part, at least part of hydrogenin the material mixture gas is reacted with the chlorofluoroolefin.Further, the hydrogen introduction part on the most downstream side inthe gas flow direction is preferably provided at a position such thathydrogen introduced from this hydrogen introduction part can besufficiently reacted with the unreacted chlorofluoroolefin, in thecatalyst layer between this hydrogen introduction part and the gasdischarge part.

In a case where at least two catalyst layers are continuously providedin the reactor, as a method of introducing hydrogen, for example, amethod may be mentioned in which a part of hydrogen is introducedtogether with the chlorofluoroolefin from the gas introduction part inthe first catalyst layer, and the rest of hydrogen is introduced fromthe hydrogen filling part of the second or subsequent catalyst layer.

As a method of suppressing the maximum temperature of the catalyst layerto be a desired temperature other than the method (α1), a method (method(α2)) of making an inert gas flow together with the chlorofluoroolefinand hydrogen in the catalyst layer may be mentioned. By making an inertgas flow and controlling the concentrations of the chlorofluoroolefinand hydrogen flowing in the catalyst layer, an excessive temperatureincrease of the catalyst layer by the heat of reaction can besuppressed. Further, it is possible to use a diluent gas other than theinert gas instead of the inert gas or together with the inert gas.

The inert gas may, for example, be a nitrogen gas, a rare gas or Freoninert to the hydrogenation reaction. The diluent gas other than theinert gas may, for example, be hydrogen chloride.

The amount of the inert gas introduced to the catalyst layer ispreferably at least 0.1 mol, more preferably at least 0.5 mol per 1 molof the chlorofluoroolefin, whereby the maximum temperature of thecatalyst layer is likely to be kept low, formation of an over-reducedproduct as a by-product is likely to be suppressed, and deterioration ofthe catalyst is likely to be suppressed. The amount of the inert gasintroduced is preferably at most 10 mol, more preferably at most 4 molper 1 mol of the chlorofluoroolefin, in view of the inert gas recoveryratio.

As a method of suppressing the maximum temperature of the catalyst layerto be a desired temperature other than the method (α1) and the method(α2), a method (method (α3)) of adjusting the temperature of a heatmedium to heat the reactor to be a lower temperature, setting the dewpoint of the material mixture gas as the lower limit, may be mentioned.By keeping the temperature of the heat medium low, it is possible tomore quickly dissipate the heat of reaction, and an excessivetemperature increase of the catalyst layer can be suppressed.

In the method (α3), the lower temperature of the catalyst layer is moreadvantageous to suppress formation of an over-reduced product which ishardly separated from HFO-1234yf, as a by-product, and accordingly thetemperature of the catalyst layer is preferably higher than the dewpoint and less than 50° C. It is more preferably higher than the dewpoint and at most 30° C.

To suppress the maximum temperature of the catalyst layer to be adesired temperature, it is preferred to employ the method (α1), (α2) or(α3), or to employ two or three of them in combination.

The reaction pressure is preferably ordinary pressure in view of thehandling efficiency. The contact time of the chlorofluoroolefin gas tothe catalyst is preferably from 4 to 60 seconds, more preferably from 8to 40 seconds. This contact time is the contact time of thechlorofluoroolefin gas as calculated from the amount of the gasintroduced to the reactor and the volume of the catalyst layer.

With a view to suppressing formation of an over-reduced product as aby-product, the proportion of hydrogen to the chlorofluoroolefinintroduced to the catalyst layer is, as represented by the ratio (H₂/Cl)of the total number of moles of hydrogen to the number of moles ofchlorine atoms in the chlorofluoroolefin, preferably at most 0.7, morepreferably at most 0.6, further preferably at most 0.5. Further, theratio (H₂/Cl) is preferably at least 0.1, more preferably at least 0.2,in view of the yield of the reaction product.

In the method (α), the linear velocity u of the chlorofluoroolefin gasrepresented by the following formula (8) in the catalyst layer ispreferably from 0.1 to 100 cm/sec, more preferably from 1 to 30 cm/sec.This linear velocity u is the linear velocity of the chlorofluoroolefingas calculated from the amount of the gas introduced to the reactor andthe volume of the catalyst layer. When the linear velocity u of thechlorofluoroolefin gas is at least the lower limit, the productivitywill improve. When the linear velocity u of the chlorofluoroolefin gasis at most the upper limit, the reactivity of the chlorofluoroolefin andhydrogen will improve.

u=(W/100)×V/S   (8)

wherein W is the concentration (mol %) of the chlorofluoroolefin gas inthe entire gas flowing in the catalyst layer, V is the flow rate(cm³/sec) of the entire gas flowing in the catalyst layer, and S is thecross-sectional area (cm²) of the catalyst layer relative to the gasflow direction.

As the reactor used in the method (α), a known reactor capable offorming a catalyst layer when packed with the catalyst may be mentioned.

The material of the reactor may, for example, be glass, iron, nickel oran alloy containing any of them as the main component.

The produced gas after the reaction contains, in addition to the aimedhydrofluoroolefin, unreacted material, a reaction intermediate andhydrogen chloride.

Hydrogen chloride contained in the produced gas can be removed byblowing the produced gas into an aqueous alkali solution forneutralization. The alkali in the aqueous alkali solution may, forexample, be sodium hydroxide or potassium hydroxide.

As a method for separating the hydrofluoroolefin and the unreactedchlorofluoroolefin from the produced gas, for example, a known methodsuch as distillation may be employed.

The chlorofluoroolefin separated from the produced gas after thereaction can be recycled. For example, separated HCFO-1224yd may bereacted with hydrogen as a chlorofluoroolefin together with CFO-1214ya,or only HCFO-1224yd may be reacted with hydrogen independently fromCFO-1214ya.

In a case where a mixture of CFO-1214ya and HCFO-1224yd is used as thechlorofluoroolefin, since HCFO-1224yd is an intermediate when HFO-1234yfis obtained from CFO-1214ya, usually, a mixture with a low proportion ofHCFO-1224yd is used. Accordingly, the proportion of HCFO-1224yd based onthe total amount of CFO-1214ya and HCFO-1224yd is preferably at most 50mol %, more preferably at most 25 mol %.

<Method (β)>

In the method (β), a medium is preferably used. The medium may, forexample, be water or an organic solvent such as an alcohol.

The amount of the medium used is preferably from 10 to 100 parts by massper 100 parts by mass of the chlorofluoroolefin.

As a method of supplying hydrogen, a method of blowing a hydrogen gas toa liquid containing the catalyst-supporting carrier and thechlorofluoroolefin and the medium used as the case requires, or a methodof adding a medium having hydrogen preliminarily dissolved bypressurization to a liquid containing the catalyst-supporting carrierand the chlorofluoroolefin may, for example, be mentioned.

The reaction of the chlorofluoroolefin and hydrogen in the method (β)may be conducted by batch or continuously.

The reaction temperature in the method (β) is preferably from 0 to 150°C., more preferably from 20 to 100° C. When the reaction temperature isat least the lower limit, the reactivity of the chlorofluoroolefin andhydrogen will improve. When the reaction temperature is at most 150° C.,formation of an over-reduced product as a by-product is likely to besuppressed.

The reaction pressure in the method (β) is preferably from 0.01 to 5MPaG, more preferably from 0.1 to 1 MPaG by the gauge pressure. Thereaction time in the method (β) is preferably from 1 to 50 hours in thecase of the batch reaction, and is preferably from 1 to 60 seconds inthe case of the continuous reaction.

The amount of hydrogen supplied in the method (β) is such that the ratio(H₂/Cl) of the number of moles of hydrogen supplied to the number ofmoles of chlorine atoms in the chlorofluoroolefin is preferably at most0.7, more preferably at most 0.6, further preferably at most 0.5,whereby formation of an over-reduced product as a by-product is likelyto be suppressed. Further, the ratio (H₂/Cl) is preferably at least 0.1,more preferably at least 0.2, in view of the yield of HFO-1234yf. Theamount of hydrogen supplied means the amount of hydrogen dissolved inthe reaction liquid.

The reaction liquid after the reaction contains, in addition to theaimed hydrofluoroolefin, unreacted material, a reaction intermediate andhydrogen chloride. Hydrogen chloride contained in the reaction liquidcan be removed by neutralization by addition of an alkali to thereaction liquid. The alkali may, for example, be sodium hydroxide orpotassium hydroxide.

The alkali may be preliminarily added to the reaction liquid used forthe reaction.

As a method of separating the hydrofluoroolefin and the unreactedchlorofluoroolefin from the reaction liquid, for example, a known methodsuch as distillation may be employed.

The chlorofluoroolefin separated from the reaction liquid can berecycled. For example, HCFO-1224yd separated may be reacted withhydrogen as the material chlorofluoroolefin together with CFO-1214ya, oronly HCFO-1224yd separated from CFO-1214ya may be reacted with hydrogen.

As the reactor used in the method (β), a known reactor in which thereaction materials can be brought into contact with each other and aresubjected to a liquid phase reaction in the presence of the catalyst maybe mentioned.

The material of the reactor may, for example, be glass, iron, nickel oran alloy containing any of them as the main component.

[Advantageous Effects]

As described above, by using the above-described alloy catalystsupported on a carrier, a hydrofluoroolefin can be obtained withformation of an over-reduced product as a by-product suppressed.

It is estimated that by forming palladium or platinum and a specificsecond element into an alloy, the hydrogen reducing activity of theplatinum group metal is reduced, and formation of an over-reducedproduct as a by-product is suppressed, and as a result, the selectivityfor the aimed product can be improved. The mechanism is estimated asfollows.

Metals such as the platinum group element and the second element havedifferent hydrogen chemical adsorption ability (New Catalyst Chemistry,second edition, published by SANKYO SHUPPAN Co., Ltd., “Metal AdsorptionAbility” in Table 8-1, at page 181). Whether hydrogen is easily adsorbedon the surface of the platinum group metal or not in the catalyticreaction which occurs on the surface influences the catalytic activity.

The second element used in the present invention has lower hydrogenchemical adsorption ability than the platinum group metal. Accordingly,it is considered that in the present invention, by forming the platinumgroup element and the second element into an alloy, the hydrogenadsorption power of the surface of the platinum group metal issuppressed. Since the hydrogen adsorption power of the surface of theplatinum group metal is suppressed, the catalytic activity of theplatinum group metal is suppressed. As a result, excessive hydrogenreducing activity of the platinum group metal is decreased, whereby theselectivity for the aimed product will improve, and formation of anover-reduced product as a by-product is suppressed.

As described above, according to the production method of the presentinvention, a high purity hydrofluoroolefin having a low concentration ofan over-reduced product can be produced.

EXAMPLES

Now, the present invention will be described in further detail withreference to Examples and Comparative Examples. However, the presentinvention is by no means restricted to such specific Examples.

Preparation Example 1 Preparation of CFO-1214ya:

CFO-1214ya was prepared by the following method using AK225 as areaction material.

Into a glass reactor having an internal capacity of 1L equipped with aDimroth condenser cooled to 0° C., 3 g of TBAB as a phase transfercatalyst, 83 g (1.485 mol) of potassium hydroxide, 180 g of water and609 g (3.0 mol) of AK225 were charged, gradually heated with stirringand reacted at 45° C. for 1 hour. Then, a reaction crude liquidseparated into an organic phase and an aqueous phase was subjected toliquid separation, and the organic phase was subjected to distillationby a distillation column having a capacity of 1L and a number oftheoretical plate of 10. As a result of distillation, 262 g (1.43 mol)of CFO-1214ya (boiling point: 45° C.) with a purity of 99.5% wasobtained.

Example 1 Preparation of HFO-1234yf:

For preparation of HFO-1234yf, a reaction apparatus 101 shown in FIG. 1was used.

The reaction apparatus 101 comprises two reaction tubes 110A and 110B,and a salt bath 130 in which the tubes are dipped. The reaction tube110A has two catalyst packing parts 113 a and 114 a on the inlet 111 aside and on the outlet 112 a side. Likewise, the reaction tube 110B hastwo catalyst packing parts 113 b and 114 b on the inlet 111 b side andon the outlet 112 b side. The outlet 112 a of the reaction tube 110A andthe inlet 111 b of the reaction tube 110B are connected by piping.

As each of the reaction tubes 110A and 110B, a reaction tube made ofInconel (registered trademark) 600 having an inner diameter of 2.54 cmand a length of 100 cm was used. Further, using, as a carrier, activatedcarbon (BET specific surface area: 1,100 m²/g), platinum and gold weremade to be supported by a known method using chloroplatinic acid andgold chloride, followed by heat treatment in a nitrogen gas stream at500° C. for 3 hours to conduct alloying thereby to produce acatalyst-supporting carrier. The obtained catalyst-supporting carrierwas a palladium/gold catalyst-supporting activated carbon (hereinafterreferred to as “Pd—Au/C”) having 0.5 part by mass of a palladium/goldalloy (palladium:gold=90:10 (mass ratio)) catalyst supported on 100parts by mass of activated carbon. The catalyst packing part 114 a onthe outlet 112 a side of the reaction tube 110A was packed with Pd—Au/Cto form a catalyst layer 112A having a height of 40 cm. Likewise, thecatalyst packing parts 113 b and 114 b on the inlet 111 b side and onthe outlet 112 b side of the reaction tube 110B were respectively packedwith Pd—Au/C to form catalyst layers 120B and 120C each having a heightof 40 cm. The packing density of Pd—Au/C in each of the catalyst layers120A to 120C was 0.73 g/cm^(3.)

The reaction tubes 110A and 110B were dipped in the salt bath 130 sothat the catalyst layers 120A to 120C were entirely dipped, and thecatalyst layers 120A to 120C were heated to 80° C.

The chlorofluoroolefin gas (A) composed of CFO-1214ya obtained inPreparation Example 1, a hydrogen gas (B) and a nitrogen gas (C) weremade to flow through the reaction tubes 110A and 110B so that the totalmolar ratio would be hydrogen/CFO-1214ya/nitrogen=1/1/2. The contacttime of the chlorofluoroolefin gas (A) to the catalyst layers 120A to120C was 18 seconds, and the linear velocity u of the chlorofluoroolefingas (A) was 7 cm/sec. Further, 50% of the hydrogen gas (B) wasintroduced together with the chlorofluoroolefin gas (A) from the inlet111 a of the reaction tube 110A, and the rest was introduced to a pipingportion connecting the reaction tube 110A and the reaction tube 110B.That is, the hydrogen gas (B) was introduced as divided into thecatalyst layer 120A (at 0 cm point) and the catalyst layer 120B (at 40cm point) in a catalyst layer (catalyst layer length: 120 cm) consistingof the catalyst layers 120A to 120C.

The maximum temperatures of the catalyst layers 120A to 120C during thereaction were measured respectively by bulk thermometers 140A to 140Cinserted to the respective catalyst layers.

A produced gas (D) discharged from the outlet 112 b of the reaction tube110B of the reaction apparatus 101 was analyzed by gas chromatography(hereinafter referred to as “GC”), whereupon the content of HFC-254ebwas 5.5 vol %, and the content of HFO-1243zf based on HFO-1234yf was 290vol ppm.

Example 2

The reaction was carried out in the same manner as in Example 1 exceptthat as the catalyst-supporting carrier, instead of Pd—Au/C, apalladium/cupper catalyst-supporting activated carbon (hereinafterreferred to as “Pd—Cu/C”) having 0.5 part by mass of a palladium/copperalloy (palladium:copper=87:13 (mass ratio)) supported on 100 parts bymass of the same activated carbon as in Example 1 was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 6.3 vol %, and the content of HFO-1243zf based onHFO-1234yf was 0 vol ppm.

Example 3

The reaction was carried out in the same manner as in Example 1 exceptthat as the catalyst-supporting carrier, instead of Pd—Au/C, apalladium/tin catalyst-supporting activated carbon (hereinafter referredto as “Pd—Sn/C”) having 0.5 part by mass of a palladium/tin alloy(palladium:tin=78:22 (mass ratio)) supported on 100 parts by mass of thesame activated carbon as in Example 1 was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 8.4 vol %, and the content of HFO-1243zf based onHFO-1234yf was 0 vol ppm.

Example 4

The reaction was carried out in the same manner as in Example 1 exceptthat as the catalyst-supporting carrier, instead of Pd—Au/C, apalladium/bismuth catalyst-supporting activated carbon (hereinafterreferred to as “Pd—Bi/C”) having 0.5 part by mass of a palladium/bismuthalloy (palladium:bismuth=67:33 (mass ratio)) supported on 100 parts bymass of the same activated carbon as in Example 1 was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 2.3 vol %, and the content of HFO-1243zf based onHFO-1234yf was 0 vol ppm.

Comparative Example 1

The reaction was carried out in the same manner as in Example 1 exceptthat as the catalyst-supporting carrier, instead of Pd—Au/C, apalladium/ruthenium catalyst-supporting activated carbon (hereinafterreferred to as “Pd—Ru/C”) having 0.5 part by mass of apalladium/ruthenium alloy (palladium:ruthenium=80.8:19.2 (mass ratio))supported on 100 parts by mass of the same activated carbon as inExample 1 was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 18.4 vol %, and the content of HFO-1243zf based onHFO-1234yf was 0 vol ppm.

Comparative Example 2

The reaction was carried out in the same manner as in Example 1 exceptthat as the catalyst-supporting carrier, instead of Pd—Au/C, a palladiumcatalyst-supporting activated carbon (hereinafter referred to as “Pd/C”)having 0.5 part by mass of palladium supported on 100 parts by mass ofthe same activated carbon as in Example 1 was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 10.1 vol%, and the content of HFO-1243zf based onHFO-1234yf was 1,220 vol ppm.

Example 5

The reaction was carried out in the same manner as in Example 1 exceptthat as the carrier, a palladium/gold catalyst-supporting γ-alumina(hereinafter referred to as “Pd—Au/γ-Al”) using γ-alumina (BET specificsurface area:130 m²/g) instead of activated carbon, was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 10.0 vol %, and the content of HFO-1243zf based onHFO-1234yf was 610 vol ppm.

Comparative Example 3

The reaction was carried out in the same manner as in ComparativeExample 2 except that as the carrier, a palladium catalyst-supportingγ-alumina (hereinafter referred to as “Pd/Al”) using γ-alumina (BETspecific surface area:130 m²/g) instead of activated carbon, was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 17.2 vol %, and the content of HFO-1243zf based onHFO-1234yf was 700 vol ppm.

Example 6

The reaction was carried out in the same manner as in Example 1 exceptthat as the carrier, a palladium/gold catalyst-supporting α-alumina(hereinafter referred to as “Pd—Au/α-Al”) using α-alumina (BET specificsurface area:12 m²/g) instead of activated carbon, was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 7.3 vol %, and the content of HFO-1234zf based onHFO-1234yf was 45 vol ppm.

Comparative Example 4

The reaction was carried out in the same manner as in Example 1 exceptthat as the carrier, a palladium catalyst-supporting α-alumina(hereinafter referred to as “Pd/α-Al”) using α-alumina (BET specificsurface area:12 m²/g) instead of activated carbon, was used.

The produced gas (D) was analyzed by GC, whereupon the content ofHFC-254eb was 25.8 vol %, and the content of HFO-1234zf based onHFO-1234yf was 125 vol ppm.

The conditions, and the content of HFC-254eb and the content ofHFO-1243zf based on HFO-1234yf in the produced gas (D) in Examples 1 to6 and Comparative

Examples 1 to 4 are shown in Table 1.

TABLE 1 Amount of Content of catalyst HFO-1234zf supported Pd:anotherContent of based on based on carrier element HFO-254eb HFO-1234yfCatalyst (mass %) (mass ratio) Carrier (vol %) (vol ppm) Example 1 Pd—Au0.5 90:10 Activated 5.5 290 carbon Example 2 Pd—Cu 0.5 87:13 Activated6.3 0 carbon Example 3 Pd—Sn 0.5 78:22 Activated 8.4 0 carbon Example 4Pd—Bi 0.5 67:33 Activated 2.3 0 carbon Comparative Pd—Ru 0.5 81:19Activated 18.4 0 Example 1 carbon Comparative Pd 0.5 100:0  Activated10.1 1220 Example 2 carbon Example 5 Pd—Au 0.5 91:10 γ-alumina 10.0 610Comparative Pd 0.5 100:0  γ-alumina 17.2 700 Example 3 Example 6 Pd—Au0.5 91:10 α-alumina 7.3 45 Comparative Pd 0.5 100:0  α-alumina 25.8 125Example 4

As shown in Table 1, in Examples 1 to 4 in which a catalyst-supportingcarrier having an alloy of palladium and each second element supportedon activated carbon was used, formation of HFC-254eb and HFO-1243zfwhich are over-reduced products as by-products was suppressed ascompared with Comparative Example 1 in which a catalyst-supportedcarrier having an alloy of palladium and ruthenium supported onactivated carbon was used and Comparative Example 2 in which the secondelement was not employed. Particularly in a case where as thecatalyst-supporting carrier, Pd—Cu/C (Example 2), Pd—Sn/C (Example 3) orPd—Bi/C (Example 4) was used, the content of HFO-1243zf based onHFO-1234yf was 0 ppm and was remarkably low, while the content ofHFC-254eb was kept to be so low as at most 8.4 vol %.

Further, in Examples 5 and 6 in which a catalyst-supporting carrierhaving an alloy of palladium and gold supported on γ-alumina orα-alumina was used, formation of HFC-254eb and HFO-1243zf which areover-reduced products as by-products was suppressed as compared withComparative Examples 3 and 4 in which the second element such as goldwas not used.

INDUSTRIAL APPLICABILITY

A hydrofluoroolefin obtained by the production method of the presentinvention has high purity with formation of an over-reduced product as aby-product suppressed. Accordingly, the obtained hydrofluoroolefin canbe used as e.g. a refrigerant which replaces Freon such as achlorofluorocarbon without any purification/separation means.

This application is a continuation of PCT Application No.PCT/JP2015/073748 filed on Aug. 24, 2015, which is based upon and claimsthe benefit of priority from

Japanese Patent Application No. 2014-170502 filed on Aug. 25, 2014. Thecontents of those applications are incorporated herein by reference intheir entireties.

REFERENCE SYMBOLS

101: reaction apparatus, 120A to 120C: catalyst layer, A:chlorofluoroolefin gas, B: hydrogen gas, C: nitrogen gas, D: producedgas

What is claimed is:
 1. A method for producing a hydrofluoroolefin, whichcomprises reacting a chlorofluoroolefin represented by the followingformula (1) with hydrogen in the presence of a catalyst supported on acarrier, to obtain a hydrofluoroolefin represented by the followingformula (2), wherein the catalyst is a catalyst composed of an alloycontaining at least one platinum group element selected from the groupconsisting of palladium and platinum, and at least one second elementselected from the group consisting of manganese, copper, aluminum, gold,lithium, sodium, potassium, magnesium, silver, zinc, cadmium, indium,silicon, germanium, tin, lead, arsenic, antimony and bismuth:CZX═CClY  (1) wherein X is a fluorine atom or a chlorine atom, Y is afluorine atom, a chlorine atom or a hydrogen atom, and Z is a fluorineatom or CF₃;CZX′═CHY′  (2) wherein X′ is a fluorine atom when X is a fluorine atom,or X′ is a hydrogen atom when X is a chlorine atom, Y′ is a fluorineatom when Y is a fluorine atom, or Y′ is a hydrogen atom when Y is achlorine atom or a hydrogen atom, and Z is the same as Z in the formula(1).
 2. The method for producing a hydrofluoroolefin according to claim1, wherein the second element is at least one member selected from thegroup consisting of copper, gold, tin, antimony and bismuth.
 3. Themethod for producing a hydrofluoroolefin according to claim 1, whereinthe content ratio of the platinum group element to the second element(platinum group element:second element) in the alloy is from 60:40 to99:1 by mass ratio.
 4. The method for producing a hydrofluoroolefinaccording to claim 1, wherein the catalyst is a catalyst composed of analloy of palladium and at least one second element selected from thegroup consisting of copper, gold, tin, antimony and bismuth.
 5. Themethod for producing a hydrofluoroolefin according to claim 1, whereinthe carrier is at least one member selected from the group consisting ofactivated carbon, carbon black and carbon fibers.
 6. The method forproducing a hydrofluoroolefin according to claim 1, wherein the carrieris at least one member selected from the group consisting of alumina,silica, titanic and zirconia.
 7. The method for producing ahydrofluoroolefin according to claim 1, wherein the amount of thecatalyst supported is from 0.1 to 10 mass % based on the carrier.
 8. Themethod for producing a hydrofluoroolefin according to claim 1, whereinthe chlorofluoroolefin and hydrogen are introduced to a catalyst layerpacked with the carrier supporting the catalyst, and reacted in agaseous phase.
 9. The method for producing a hydrofluoroolefin accordingto claim 8, wherein the chlorofluoroolefin and hydrogen are introducedto a gas introduction part of the catalyst layer, and hydrogen isintroduced from at least one point between the gas introduction part anda gas discharge part of the catalyst layer.
 10. The method for producinga hydrofluoroolefin according to claim 8, wherein the reaction iscarried out while the maximum temperature of the catalyst layer iscontrolled to be at most 130° C.
 11. The method for producing ahydrofluoroolefin according to claim 8, wherein the proportion ofhydrogen to the chlorofluoroolefin introduced to the catalyst layer isfrom 1 to 0.7 as represented by the ratio (H₂/Cl) of the total number ofmoles of hydrogen to the number of moles of chlorine atoms in thechlorofluoroolefin.
 12. The method for producing a hydrofluoroolefinaccording to claim 1, wherein the chlorofluoroolefin and hydrogen arereacted in a liquid phase in the presence of the carrier supporting thecatalyst.
 13. The method for producing a hydrofluoroolefin according toclaim 1, wherein the chlorofluoroolefin is at least one member selectedfrom the group consisting of chlorotrifluoroethylene,trans-1,2-dichloro-1,2-difluoroethylene,cis-1,2-dichloro-1,2-difluoroethylene,1,1-dichloro-2,3,3,3-tetrafluoropropene and1-chloro-2,3,3,3-tetrafluoropropene.
 14. The method for producing ahydrofluoroolefin according to claim 1, wherein2,3,3,3-tetrafluoropropene is produced from1,1-dichloro-2,3,3,3-tetrafluoropropene.